CN104557434B - The method for producing paraxylene - Google Patents
The method for producing paraxylene Download PDFInfo
- Publication number
- CN104557434B CN104557434B CN201310512755.5A CN201310512755A CN104557434B CN 104557434 B CN104557434 B CN 104557434B CN 201310512755 A CN201310512755 A CN 201310512755A CN 104557434 B CN104557434 B CN 104557434B
- Authority
- CN
- China
- Prior art keywords
- carbon
- component
- raw material
- paraxylene
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of paraxylene production method, technical problem that mainly to solve in previous Aromatic Hydrocarbon United Plant that there are dimethylbenzene circuits long, investment is big, energy consumption is high.The present invention by using come reformer unit light dydrocarbon and its more than group dispensing to raw material Disengagement zone, successively isolate carbon six and its following components, carbon seven, carbon eight and the above component；The carbon six and its following components are sent to depentanizer, and purified petroleum benzin product is obtained；Seven groups of dispensings of the carbon generate to disproportionation and transalkylation and return to raw material Disengagement zone containing benzene,toluene,xylene, carbon nine and its above aromatic hydrocarbons and the mixture of non-aromatics I；The carbon eight and its above group are distributed into benzenol hydrorefining and are separated, and obtain para-xylene product, inhale excess oil and obtain Mixed XYLENE into isomerization unit and return to raw material Disengagement zone；Tower bottom obtains carbon nine and its above group is distributed into heavy aromatics tower, and disproportionation technical solution is returned after tower top obtains carbon nine, ten component of carbon is mixed with seven component of carbon, above-mentioned technical problem is preferably solved, can be used for paraxylene industrial production.
Description
Technical field
The present invention relates to a kind of paraxylene production methods of low energy consumption.
Background technique
Paraxylene is one of main basic organic of petrochemical industry, in chemical fibre, synthetic resin, pesticide, medicine, modeling
Numerous chemical production fields such as material have extensive purposes.Utilize toluene and carbon nine and its above heavy aromatics (C9 +A) transalkylation
Reaction increasing production of xylol is the method for efficiently using heavy aromatics and carrying out increasing production of xylol, is widely used.Industrial PX product is main
It is produced by Aromatic Hydrocarbon United Plant.Traditional Aromatic Hydrocarbon United Plant includes reforming, being disproportionated and transalkylation, isomerization, aromatic hydrocarbons
Unit processes, PX and the benzene such as extracting, PX separation are produced as final products.The aromatic hydrocarbons of reformer unit production, disproportionation turn with alkyl
Shifting unit generation product successively passes through benzene column, toluene tower and benzenol hydrorefining and isolates benzene, toluene and dimethylbenzene.And isomerization unit
Product removes non-aromatic and C7 by stabilizer and deheptanizer-Benzenol hydrorefining is returned after A aromatic hydrocarbons.It is found that eight virtue of whole process carbon
Hydrocarbon need to be recycled largely, cause associated column separation process energy consumption, material consumption high.
US7304193B1 discloses a kind of integrated process flow for producing aromatic hydrocarbons, and the technique is straight by isomerization unit product
It taps into transalkylation stabilizer, extracts C from tower top6 -It organizes lease making stabilizer and enters benzene extraction unit, tower bottom product is again
Toluene, dimethylbenzene and heavy aromatics are isolated by toluene tower, benzenol hydrorefining, wherein toluene and heavy aromatics return to transalkylation list
Member.The process reduces feed separation towers, not only save equipment investment, can also reduce operating cost.
US20080067053A1 discloses a kind of method for producing dimethylbenzene, by transalkylation reaction and xylene isomerization
Change reaction to be integrated, transalkylation reaction and xylene isomerization reaction can be carried out in same reaction zone, reaction product warp
Stabilizer isolates C6、C7And C8 +A, C6 obtain purified petroleum benzin product through benzene column, and C7 is as transalkylation raw material, and C8+A is through two
Toluene tower and heavy aromatics tower isolate dimethylbenzene and heavy aromatics, and heavy aromatics returns to transalkylation, dimethylbenzene warp as raw material
The C8 aronmatic and return transalkylation of poor PX after adsorbing separation, wherein C8 +A represents the aromatic hydrocarbons of eight or more carbon.
Summary of the invention
The technical problem to be solved by the present invention is in existing Aromatic Hydrocarbon United Plant there are dimethylbenzene circuit is longer, energy consumption,
The higher problem of material consumption provides a kind of paraxylene production method of low energy consumption.This method is used in paraxylene production process,
Have the advantages that cost of investment is low, energy and material consumption is low.
In order to solve the above technical problems, the present invention is as follows using technical solution, a kind of paraxylene production method is successively wrapped
Include following steps:
A) from reformer unit light dydrocarbon and its more than group dispensing to raw material Disengagement zone, isolate carbon six and its successively with the following group
Divide, seven component of carbon, carbon eight and its above component.
B) carbon six in step a) and its following components are sent to depentanizer, and depentanizer top obtains light dydrocarbon and its with the following group
Point, tower bottom obtains six groups of dispensings of carbon to extraction unit, obtains purified petroleum benzin product.
C) seven groups of dispensings of the carbon in step a) to disproportionation and transalkylation, occur disproportionated reaction, transalkylation reaction,
Dealkylation and non-aromatics cracking reaction are generated containing benzene,toluene,xylene, carbon nine and its above aromatic hydrocarbons and non-aromatics
Mixture I.
D) the raw material Disengagement zone in the I return step a) of mixture
E) carbon eight in step a) and its above group are distributed into benzenol hydrorefining and are separated, and tower top obtains dimethylbenzene, tower bottom
Obtain carbon nine and its above component.
F) carbon nine and its above group are distributed into heavy aromatics tower, and tower top obtains in carbon nine, ten component of carbon and step c)
Disproportionation and transalkylation are returned to after the mixing of seven component of carbon, tower bottom obtains carbon 11 and its above component.
G) dimethylbenzene from step e) is sent into paraxylene adsorption separation unit, obtains para-xylene product and containing to two
Eight component of carbon of toluene.
Eight groups of carbon containing paraxylene from step g) are distributed into isomerization unit, and reaction obtains Mixed XYLENE return step
A) the raw material Disengagement zone in.
In above-mentioned technical proposal, preferred technical solution, raw material Disengagement zone is made of at least one knockout tower；In step a)
Light dydrocarbon and its above component contain benzene, toluene, C8 aronmatic and at least one of carbon nine and its above heavy aromatics；In step a)
Non-aromatic content is less than 70 wt% in carbon six and its above component；Contain the carbon no more than 20 wt% in step a) in seven component of carbon
Six components；The non-aromatic content of seven component of carbon is less than 30 wt% in step a)；Benzaldehyde product purity is greater than 99.9wt%, step in step b)
It is rapid g) in para-xylene product concentration be greater than 99.8%；Disproportionation contains with catalyst used in transalkylation selected from β-boiling
At least one of stone, modenite, ZSM-12, NU-87, ZSM-5 or MCM-22 molecular sieve also contain at least one in catalyst
Kind is selected from the metal or its oxide of platinum, palladium, rhenium, molybdenum, nickel, bismuth, and dosage is 0.005 ~ 5% by weight percentage；Disproportionation with
The operating condition of transalkylation is as follows: reaction pressure is 0.5 ~ 5MPa, and reaction temperature is 200 ~ 600 DEG C, hydrogen hydrocarbon molar ratio
0.5 ~ 10, liquid weight air speed is 0.8 ~ 10h-1；The operating condition of isomerization of C-8 aromatics unit is as follows: reaction pressure be 0.5 ~
6MPa, reaction temperature are 300 ~ 500 DEG C, and hydrogen hydrocarbon molar ratio 0.5 ~ 25, liquid weight air speed is 0.5 ~ 10h-1
In technical solution of the present invention, aroamtic hydrocarbon raw material, disproportionation and transalkylated product and eight virtue of carbon from reformer unit
The unified raw material Disengagement zone that enters is separated after the mixing of olefin isomerization unit product, simplifies each unit tower separation process.Raw material
Disengagement zone extraction carbon six and its following components enter Aromatics Extractive Project after depentanizer separates and obtain purified petroleum benzin product, effectively reduce
Aromatics Extractive Project unit energy consumption.Seven component of carbon and carbon nine, ten component of carbon for containing a certain amount of non-aromatics enter discrimination as reaction raw materials
Change and transalkylation generate the product that dimethylbenzene amount increases.The present invention can be used for PX production process, has and invests low, energy
Consume the low effect of material consumption.
Detailed description of the invention
Fig. 1 is the process flow diagram for the method that low energy consumption of the invention produces paraxylene.
I is reforms depentanizer in Fig. 1, and II is raw material knockout tower, and III is disproportionation and transalkylation, and IV is deolefination
Unit, V is benzenol hydrorefining, and VI is paraxylene adsorption separation unit, and VII is isomerization of C-8 aromatics unit, and VIII is de- for raw material
Pentanizer, Ⅸ is Aromatics Extractive Project unit.1 is reforms cellular manufacture oil, and 2 be light dydrocarbon and following components, and 3 be carbon six and its above group
Point, 4 be carbon six and following components, 5 be seven component of carbon, 6 be carbon eight and the above component, 7 for disproportionation and transalkylation product,
8 for after deolefination carbon eight and the above component, 9 be C8 aronmatic, and 10 be carbon of the benzenol hydrorefining side take-off containing a small amount of naphthalene series substance
Nine, C10 aromartic, 11 be benzenol hydrorefining kettle liquid, and 12 be para-xylene product, and 13 feed for isomerization unit, and 14 be isomerization list
First product, 15 be light dydrocarbon and its following components, and 16 be six component of carbon, and 17 be purified petroleum benzin.
In the process flow of production paraxylene shown in FIG. 1, enters from reformer unit production oil 1 and reform depentanizer
I, tower top isolates light dydrocarbon and following components 2, and tower bottom carbon six and the above component 3 are into raw material knockout tower II, carbon six and with the following group
Points 6 extract from tower top, and into raw material depentanizer VIII, tower top extracts light dydrocarbon and following components 15, and six component 16 of tower bottom carbon is into benzene
Extraction unit Ⅸ obtains the benzaldehyde product 17 that purity is greater than 99.85%.Seven component 5 of carbon from II side take-off of raw material knockout tower, as
Reaction raw materials enter disproportionation and transalkylation III, and disproportionation and transalkylation product 7 return to raw material knockout tower II and carry out
Separation.Carbon eight and the above component 6 are flowed out from II bottom of raw material knockout tower, enter benzenol hydrorefining V after the processing of deolefination unit IV.
C8 aronmatic 9 is extracted from tower top, into paraxylene adsorption separation unit VI, obtains para-xylene product 12.Benzenol hydrorefining V
Side take-off containing lacked the carbon nine of naphthalene series substance, C10 aromartic 10 is recycled back to disproportionation and transalkylation III, dimethylbenzene tower reactor
11 outlet of liquid.C8 aronmatic 13 after the separation of paraxylene adsorption separation unit VI is used as reaction raw materials into isomerization unit
VII, isomerization unit product 14 returns to raw material knockout tower II and is separated.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
To reform C6 +For raw material, raw material composition is as shown in table 1.
Process flow is as shown in Figure 1.Fresh reformation C5 +Raw material 100t/h enters reformation depentanizer, and tower top deviates from C5Component
5.9t/h, tower bottom C6+ entering raw material knockout tower, raw material separates overhead extraction C6Component, into depentanizer, overhead extraction C5-
Component, tower bottom component enter Aromatics Extractive Project unit and obtain the benzaldehyde product that purity is 99.9%.Raw material knockout tower side take-off C7Component
(contain 2wt%C6Component and 3wt% non-aromatics) with the C of heavy aromatics tower side take-off9-C10Aromatic hydrocarbons and hydrogen mixing after enter disproportionation with
Transalkylation, reaction liquid product return to raw material knockout tower.Raw material knockout tower bottom group lease making deolefination cell processing is laggard
Enter benzenol hydrorefining, dimethylbenzene overhead extraction 123.5t/h dimethylbenzene enters paraxylene adsorption separation unit, and it is pure to obtain 99.8wt%
Paraxylene is spent, extraction raffinate is inhaled and enters the C8 aronmatic component of isomerization unit reaction generation thermodynamical equilibrium, and return to raw material point
From tower.Benzenol hydrorefining bottom C11+ component (6.8t/h) outlet.
Disproportionation uses fixed bed reactors with transalkylation, and filling is load weight than meter 0.1% in reactor
The beta zeolite and ZSM-5 zeolite mixed catalyst of Pt.Isomerization unit uses fixed bed reactors, and filling contains Pt in reactor
For 0.2% mordenite catalyst, see Table 2 for details for the prevailing operating conditions of each reaction member, and reaction product is shown in Table 3.
Table 1
Table 2
Table 3
| Product | Yield (t/h) |
| C5- | 5.9 |
| Benzene | 25.1 |
| Paraxylene | 45.6 |
| It raffinates oil | 16.6 |
| C11+ A heavy aromatics | 6.8 |
[embodiment 2]
To reform C9 +For raw material, raw material composition is as shown in table 4.
Process flow is as shown in Figure 1.Fresh reformation C9 +Raw material 100t/h enters raw material knockout tower, and raw material separates overhead extraction
C6Component, into depentanizer, overhead extraction C5Component, it is 99.9% that tower bottom component, which enters Aromatics Extractive Project unit to obtain purity,
Benzaldehyde product.Raw material knockout tower side take-off C7Component (contains 1wt%C6Component and 2wt% non-aromatics) and heavy aromatics tower side take-off
C9-C10Enter disproportionation and transalkylation after aromatic hydrocarbons and hydrogen mixing, reaction liquid product returns to raw material knockout tower.Raw material point
From benzenol hydrorefining is entered after tower bottom group lease making deolefination cell processing, dimethylbenzene overhead extraction dimethylbenzene enters paraxylene absorption
Separative unit obtains 99.8wt% purity para-xylene, inhales extraction raffinate and enters the carbon eight that isomerization unit reaction generates thermodynamical equilibrium
Aromatic component, and return to raw material knockout tower.Benzenol hydrorefining bottom C11+ component outlet.
Disproportionation uses fixed bed reactors with transalkylation, and filling is load weight than meter 0.2% in reactor
The mordenite catalyst of Pt.Isomerization unit uses fixed bed reactors, and filling EU-1 for being 0.2% containing Pt boils in reactor
Stone catalyst, see Table 5 for details for the prevailing operating conditions of each reaction member, and reaction product is shown in Table 6.
Table 4
Table 5
Table 6
| Product | Yield (t/h) |
| C5- | 7.5 |
| Benzene | 23.1 |
| Paraxylene | 46.0 |
| It raffinates oil | 15.6 |
| C11+ A heavy aromatics | 7.8 |
Claims (6)
1. a kind of paraxylene production method, successively the following steps are included:
A) come reformer unit light dydrocarbon and its more than group dispensing to raw material Disengagement zone, successively isolate carbon six and its following components,
Seven component of carbon, carbon eight and its above component；
B) carbon six and its following components are sent to depentanizer, and depentanizer top obtains light dydrocarbon and its following components, and tower bottom obtains carbon
Six groups of dispensings obtain purified petroleum benzin product to extraction unit；
Disproportionated reaction, transalkylation reaction, de- alkyl occur for seven groups of dispensings of carbon described in c) anti-to disproportionation and transalkylation
It answers and non-aromatics cracking reaction, generation contains benzene,toluene,xylene, carbon nine and its above aromatic hydrocarbons and the mixture of non-aromatics I；
D) the raw material Disengagement zone in the I return step a) of mixture；
E) carbon eight in step a) and its above group are distributed into benzenol hydrorefining and are separated, and tower top obtains dimethylbenzene, and tower bottom obtains
Carbon nine and its above component；
F) carbon nine and its above group are distributed into heavy aromatics tower, and tower top obtains the carbon seven in carbon nine, ten component of carbon and step c)
Disproportionation and transalkylation are returned to after component mixing, tower bottom obtains carbon 11 and its above component；
G) dimethylbenzene from step e) is sent into paraxylene adsorption separation unit, obtains para-xylene product and containing paraxylene
Eight component of carbon；
H) eight groups of carbon containing paraxylene from step g) are distributed into isomerization unit, and reaction obtains Mixed XYLENE return step a)
In raw material Disengagement zone；
Wherein the non-aromatic hydrocarbon content in step a) in seven component of carbon is less than 30wt%；
Disproportionation uses fixed bed reactors with transalkylation, and filling is Pt of the load weight than meter 0.1% in reactor
Beta zeolite and ZSM-5 zeolite mixed catalyst, disproportionation with transalkylation operating condition are as follows: inlet pressure 3.0MPa,
410 DEG C of inlet temperature, weight space velocity 3.0h-1, hydrogen-hydrocarbon ratio 4mol/mol.
2. paraxylene production method according to claim 1, which is characterized in that raw material Disengagement zone is by least one separation
Tower composition.
3. paraxylene production method according to claim 1, which is characterized in that light dydrocarbon and its above component in step a)
Contain benzene, toluene, C8 aronmatic and at least one of carbon nine and its above heavy aromatics.
4. paraxylene production method according to claim 1, which is characterized in that containing not in seven component of carbon in step a)
Six component of carbon greater than 20wt%.
5. paraxylene production method according to claim 1, which is characterized in that benzaldehyde product purity is greater than in step b)
Para-xylene product concentration is greater than 99.8wt% in 99.9wt%, step g).
6. paraxylene production method according to claim 1, which is characterized in that the operation of isomerization of C-8 aromatics unit
Condition is as follows: reaction pressure is 0.5~6MPa, and reaction temperature is 300~500 DEG C, hydrogen hydrocarbon molar ratio 0.5~25, liquid weight
Air speed is 0.5~10h-1。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310512755.5A CN104557434B (en) | 2013-10-28 | 2013-10-28 | The method for producing paraxylene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310512755.5A CN104557434B (en) | 2013-10-28 | 2013-10-28 | The method for producing paraxylene |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104557434A CN104557434A (en) | 2015-04-29 |
| CN104557434B true CN104557434B (en) | 2019-05-14 |
Family
ID=53074619
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310512755.5A Active CN104557434B (en) | 2013-10-28 | 2013-10-28 | The method for producing paraxylene |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104557434B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106694054A (en) * | 2016-12-16 | 2017-05-24 | 东至绿洲环保化工有限公司 | Load-type resin catalyst for preparing xylene by virtue of selective toluene disproportionation |
| US10173950B2 (en) * | 2017-01-04 | 2019-01-08 | Saudi Arabian Oil Company | Integrated process for the production of benzene and xylenes from heavy aromatics |
| CN109336731A (en) * | 2018-12-08 | 2019-02-15 | 大连福佳·大化石油化工有限公司 | Improved crude benzol production system |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1413968A (en) * | 2001-10-22 | 2003-04-30 | 中国石油化工股份有限公司 | Toluene selective disproportion and toluene and C9 and its above aromatic disproportion and alkyl transfusion method |
| CN101379012A (en) * | 2004-05-27 | 2009-03-04 | 环球油品公司 | Catalyst treatment useful for aromatics conversion process |
| CN101808963A (en) * | 2007-07-30 | 2010-08-18 | 环球油品公司 | Xylene production processes and apparatus with integrated feedstock treatment |
| CN101885661A (en) * | 2009-05-13 | 2010-11-17 | 中国石油化工股份有限公司 | Combination method for joint production of arene |
-
2013
- 2013-10-28 CN CN201310512755.5A patent/CN104557434B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1413968A (en) * | 2001-10-22 | 2003-04-30 | 中国石油化工股份有限公司 | Toluene selective disproportion and toluene and C9 and its above aromatic disproportion and alkyl transfusion method |
| CN101379012A (en) * | 2004-05-27 | 2009-03-04 | 环球油品公司 | Catalyst treatment useful for aromatics conversion process |
| CN101808963A (en) * | 2007-07-30 | 2010-08-18 | 环球油品公司 | Xylene production processes and apparatus with integrated feedstock treatment |
| CN101885661A (en) * | 2009-05-13 | 2010-11-17 | 中国石油化工股份有限公司 | Combination method for joint production of arene |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104557434A (en) | 2015-04-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101830772B (en) | Combined method for producing p-xylene | |
| CN105272805B (en) | A kind of method for producing paraxylene | |
| CN110790625B (en) | Process for producing aromatic hydrocarbons | |
| CN105272803B (en) | The method that toluene is disproportionated transalkylation with heavy aromatics | |
| CN103880584B (en) | The method of Joint Production paraxylene | |
| CN107074681A (en) | Use the high-purity paraxylene production method of a Simulation moving bed separative element and two isomerization units based on xylene fraction | |
| CN104557434B (en) | The method for producing paraxylene | |
| CN101993332B (en) | Combined method for joint production of aromatic hydrocarbon | |
| CN102190553B (en) | Aromatic hydrocarbon alkyl transfer method for producing benzene and p-xylene | |
| CN105272804B (en) | The method of accordance transfer and non-aromatic hydrocarbon pyrolysis increasing production of xylol | |
| CN104557431B (en) | The paraxylene production method of diversification of feedstock | |
| TW201323405A (en) | Process and apparatus for para-xylene production using multiple adsorptive separation units | |
| CN101734989B (en) | Method for selective toluene disproportionation and transalkylation of benzene and C9 aromatics | |
| CN101993334B (en) | Method for increasing yield of p-xylene in aromatic hydrocarbon production | |
| EP3153490A1 (en) | Method for preparing paraxylene with co-production of propylene with high selectivity | |
| CN101811926B (en) | Method for aromatic co-production | |
| CN104557430A (en) | Method for increasing xylene yield by aromatic hydrocarbon alkyl transfer and olefin removal | |
| CN103508837A (en) | Method for producing paraxylene through adsorption and crystallization process | |
| CN101993333B (en) | Combined method for increase production of paraxylene in arene production | |
| CN101811927B (en) | Method for producing paraxylene | |
| CN101885661B (en) | Combination method for joint production of arene | |
| CN104109074B (en) | The combine production method of xylol | |
| CN104557429B (en) | Diversification of feedstock produces the method for paraxylene | |
| CN101735000B (en) | Combination method for producing p-xylene | |
| CN103772128B (en) | Produce the integrated processes of p-Xylol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |